Apparatus for contacting fluids with subdivided solids



Dec. 30, 1947. c. H. ANGELI. .2,433,726

APPARATUS FOR CONTACTING-FLUIDS WITH SUBDIVIDED SOLIDS Filed Nov. 29, 1945 llllll UU Z4" n; Z6 Z7 n Il'. Z4 ne/barella?" alvarez/of ZZ ZZ rnente'd'nee. so, 1941 l UNITED STATE APPARATUS FOR C WITH SUBDIVIDED SOLIDS Charles H. Angell,

versal Oil Products corporation of Delaware Chicago, Ill., assignor to Unl- Company, Chicago, Ill., a

Application November-29, 1943, Serial No. 512,117

Y Claims. (Cl. 19d-52) The invention relates to an improved process involving contact between iluids' and subdivided solids and to an improved form of apparatus in which such a process may be conducted.

The invention is not limitedto the specific fluids and subdivided solids contacted since its features will be found advantageous as applied to numerous specific operations involving contact between various types of subdivided solid materials and fluids, for treatment of either or both the solid and the fluid materials or for effecting the conversion of one or both. However, the features of the invention are particularly advantageous as applied to the conversion of fluid hydrocarbons in contact with subdivided solid catalysts which promote the desired conversion reaction and/or retard undesirable secondary or side reactions, accompanied by continuous regeneration ofn the catalyst which becomes contaminated by the deposition thereon of deleteriousr combustible products of the conversion reaction. Regeneration of the catalyst is effected by burning combustible contaminants therefrom in a stream of oxidizing gas and the conversionreaction and regeneration of the catalyst are accomplished simultaneously in separate confined reaction and regenerating zones through which the subdivided solidcatalytic material is circulated.

The specilc reactions of catalytic cracking, dehydrogenation, aromatization, hydrogen transfer and combinations of such reactions exemplify operations of the general type to which the features of the invention are particularly directed. A description of the improved process herein provided as applied to the catalytic cracking of hydrocarbons will serve to illustrate the features and advantages of the invention and the subsequent description will therefore be to such an operation and to the improved form of apparatus in which it is conducted.

The accompanying diagrammatic drawing is an elevational view, shown principally in section, of one speciiic form of the apparatus provided by the invention and the following description of the apparatus includes a description of the mode of operation provided. l

Referring to the drawing, the apparatus here illustrated comprises a vertically elongated, substantially cylindrical vessel formed by an outer shell I, an inverted substantially conical lower head 2, an upper head 3 and having an intermediate partition 4 of inverted substantially conical form which divides the vessel into a lower compartment comprising the reaction zone 5 and directed particularlyan upper compartment comprising the regenerating zone 6.

A bed of subdivided solid catalyst or contact material indicated at 1 is maintained within the reaction zone above a perforate plateA or other suitable form of distributing grid 8 disposed at substantially the junction of the cylindrical shell I with the cone bottom 2 of the vessel. This bed is maintained in a iluid-like condition of relatively highsolid particle concentration by the upward passage therethrough of iluid reactants and resulting fluid conversion products at a velocity regulated to partially counteract the force of gravity on the solid particles of the bed and cause their hindered settling. The reactants are supplied to the lower portion of the vessel beneath the distributing grid 8 through line 9 and Valve I0 either in normally liquid or essentially vaporous state or in a mixed phase condition and they may, when desired, be preheated before being supplied to the reactor to substantially the temperature 'desired for conducting the-reaction or to any desired lower temperature.

Another bed of subdivided solid catalyst or contact material, indicated at II, is maintained within the regenerating zone above a perforate plate or suitable form of distributing grid I2 disposed at substantially the junction of shell I with the partition 4. This bed is also maintained in fluid-like condition of relatively high solid particle concentration by the upward passage therethrough of oxidizing gas employed to accomplish regeneration of the catalyst and resulting-combustion gases at a velocity regulated to partially counteract the force of gravity on the solid particles within the bed and cause their hindered settling. The regenerating gas, which preferably is air or may be air diluted withCOz, combustion gases or other suitable substantially non-oxidizing gas, is supplied to the vessel, either preheated or at substantially atmospheric temperature through line I3 vand valve I4 and thence into the regenerator, as will be later described.

By suitable control. of the rates at which fluid reactants and regenerating gas are supplied, respectively, to the reaction and regenerating zones in relation to the horizontal cross-sectional area of the beds 1 and Il, and in relation to the average particle size and weight of the subdivided solid catalyst or contact the catalyst inventory within the vessel at a substantially constant volume, together with the method and means provided for circulating and controlling circulation of the subdivided solid material between the reaction and regenerating material and by keeping 3 zones, the upper extremities of the fluid-like beds 1 and Il are each maintained at a suitable level beneath thepoints within the respective zones from which the outgoing fluid conversion products and the outgoing gaseous products of regen eration are withdrawn. The approximate upper extremity of the relatively dense fluid bed 'l is indicated at l5 and the approximate upper extremity of the relatively dense fluid bed I I is indicated at I6. By virtue of this provision, a space is maintained in the reaction and regenerating zones above the respective iluid beds 1 and Il in which the concentration of solid particles is greatly reduced as compared with that prevailing within the beds. Thus, a major separation of Y solid particles from the outgoing iiuid conversion products and regenerating gas is effected at the approximate interface between the fluid-like bed and the light phase existing above it.

Although a relatively sharp interface or line of demarcation between the uid beds and the light phases is indicated at I5 and I6 in thedrawing, this interface is more in the nature of a band or region of rapidly decreasing solid particle concentration. The density in the fluid beds may range, for example, from`5 to 30 pounds, or thereabouts, per cubic foot, while the density in the light phases adjacent the points in the reaction and regenerating zones from which iiuid conversion products and outgoing gaseous products of regeneration are discharged maybe as low as one pound or a fraction of a pound per cubic foot. The average density in the conical sections 2 and 4 of the vessel are also less than the densities in the respective beds 1 and Il due to the higher average vapor and gas velocities in these zones, the velocity decreasing and the density increasing as the vapor or gas approachesthe wide'portion of the cone.

As above indicated, iluidization of the beds and control of the interface between the bed and the light phase above itdepends `upon a number of factors. 'The diameter of the vessel or, more specically, the horizontal cross-sectional area of the bed, and the rate at which reactants and regenerating gases are supplied to the reaction and regenerating zones determine the upward velocity of the vapors and/or gases passing through the beds. This velocity in relation to the density and depth of the bed determines the pressure drop therethrough, and the density of the bed, in turn, at any given velocity is related to the average particle size and weight of the catalyst or contact Vmaterial. of given size and with avspecic catalyst or contact material, both of which factors are fixed in any given operation, there isa critical vapor or gas velocity at which the. particles begin to be agitated or lifted and iiuidization of the bed begins to take place. Beyond this point an 'increase in the vapor or gas velocity causes no substantial pressure drop through the bed, but an increased velocity beyond this point will decrease the density or solid particle concentration of the bed. Thus, the preferred condition for operation of the process provided by the invention with iluidization of the beds is `with a velocity somewhat above the aforementioned critical value and this can be determined by measurement of the pressure drop through the bed. It has been found that the critical velocity is reached when.

the pressure drop through the bed is approximately equivalent to the bulk 'density of the bed. Thus, in a vessel of given size for any given average particlesize and Weight of the catalyst Thus, in a vessel or contact material, the minimum velocity required to iluidize a bed of Athe desired depth can be determined and the rates at which reactants and regenerating gas are supplied to the vessel can be adjusted to give the desired degree vof fiuidization.

To insure that the upper extremities of the uid beds are maintained beneath the gas and vapor outlets so as to insure maintenance of the desired two-phase condition within the reaction and regenerating zones, solid particles to be transferred from the regenerator to the reactor are withdrawn from beneath the desired upper extremity of the fluid bed II and solid particles to be transferred from the reactor to the regenerator are withdrawn from beneath the desired upper extremity of the fluid bed 1. In addition, it is necessary to keep the rate at which the solid particles are passed from the reaction zone to the regenerating zone substantially the same as the rate at which they are returned from the regenerating zone to the reaction zone. In the case here illustrated, these features of the operation are accomplished by providing one or a plurality of suitable transfer conduits or standpipes, indicated at I1, extending froman elevation within and preferably adjacent the upper extremity of bed II in the regenerating zone downwardly to a suitable lower point within bed 'l in the reaction zone or, as in the case illustrated, to within the zone of higher velocity and lower solid particle concentration defined by cone bottom 2 of the vessel. Conduits Il are open at their upper ends to admit solid particles from the bed Il and a suitable flow regulating valve, indicated at I8, is provided adjacent the lower end of each of these transfer lines to give a slight drop in pressure at the discharge end of conduits I1 and control the rate of circulation throughthese conduits. To complete the cycle of catalyst or contact material, transfer lines or conduits I9 and 20 are provided. Conduit I9 extends from a suitable point in bed 'I beneath and preferably adjacent its upper extremity I5 to a relatively low point in the vessel beneath the distributing member 8 and is provided adjacent its lower end with a ow regulating device 2|. The downcoming relatively dense column of catalyst or contact material passes over the upper surface of member 2i into the' incoming stream of regenerating gas supplied through line I3 to be picked up by thelatter and transported principally by its gas-lift action through conduit20 into the conical lower section 4 of the regenerator. Member 2l also maintains a slight pressure drop at the discharge end of conduit I9.

The density of the columns of solid particles in conduits I7 is greater than the density in bed 1 and the height of the columns in conduits I1 is suflcient to insure a higher hydrostatic pressure at their discharge ends than that prevailing in the zone into which they discharge. The solid particles from conduits I1 meet and are dispersed in the stream of incoming fluid reactants supplied through line 9 and the latter carry the'solid particles through' the distributing member 8 into the fluid bed wherein desired conversion of the reactants is accomplished in the presence of the relatively concentrated lmass of solid particles. The mechanism whereby solid particles are transferred from bed 'I to bed II is the same in principle as above described for transferring solid particles from bed I'I to bed 1. The density and height of the column of solid particles in conduit I9 gives a higher Vhydrostatic pressure at its disportion of the heat evolved by burning of the com-l bustibles is stored in the subdivided solid particles -and supplied therewith to the reaction zone to furnish all or a substantial portion of the heat required for conducting the conversion reaction.

One or a plurality of separators of the centrifugal or cyclone type, indicated at 22, is provided in the upper portion of the reaction section of the vessel to effect a more complete separation of solid particles from the outgoing stream of uid conversion products. The vapors or gases and entrained solid particles enterthe cyclone separators 22, as indicated by the arrows, from the light phase in the reaction zone above bed 1 and solid particles separated therein are returned through standpipes 23 to bed 1, The vapors and gases from which substantially all of the solid particles rected through conduits 24 into an outlet compartment or header 25 from which the fluid conversion products are directed through line 26 and the pressure control valve 21 to suitable fractionating and recovery equipment which does not constitute a novel part of the invention and is not illustrated.

A similar separator, preferably of the centrifugal or cyclone type is disposed, as indicated at 28, in the upper portion of the regenerating section of the vessel and receives outgoing combustion gases and entrained solid particles from the light.

phase above the fluid bed II in this zone. The separated solid particles are returned from sepahave been separated are dispace 45 between rator 28lthrough standpipe 29 to bed II. The

combustion gases are directed from the separator through line 30 and the pressure control valve 3|, preferably to suitable heat recovery equipment, not illustrated, such as, for example, a steam generator and/or superheater, hot gas turbine or the like, provided for the recovery -of useful heat energy from these gases.

To prevent the transfer of occluded oxidizing gas and combustion gases through conduits I1 into the reaction zone with the solid particles being transferred thereto from the regenerator, suitable stripping gas is introduced into these conduits at one or a plurality of points on the lpstream sides of valves I8. This stripping gas may comprise, for example, steam or other suitable relatively inert or non-oxidizing gas and its ipward passage through conduits I1 in relatively small quantities serves to prevent excessive compaction of the columns of solid particles in these lines so as to insure theiiow of solid particles therethrough. The rate at which stripping gas is supplied is regulated to accomplish the aforesaid purposes without excessive fluidization of the columns so that the density of the latter remains relatively high. Lines 32 and valves 33 are provided, in the case illustrated, for the introduction of stripping and aerating gas into conduits I1.

In a similar manner, suitable stripping and aerating gas, such as steam, for example, is supplied through line 34 and valve 35 to conduit I9 beneath the flow control member 2l and is directed through a relatively small concentric the flow control member and conduit I9 upwardly into the downwardly moving column of solid particles passing through the latter to substantially strip this column of occluded vapors and gases so as to prevent passage of the latter from the reactorinto the regenerator and to' prevent excessive compaction of the column.

It is within the scope of the invention to substitute a fixed orifice or the like adjacent the lower end of conduits I1 for the flow control valves I8 and/or to substitute a fixed orifice or the like adjacent the lower end of conduit I9 for the flow regulating device 2l. Preferably, however, to permit variation of the rate at which solid particles are transferred between. the reaction and regenerating zones, an adjustable flow regulating device is provided either at the lower end of conduits I1 or adjacent the lower end of conduit I9, or both.

In the case illustrated, valves I8 are of special construction which avoids packing vof the valve stems 3B where the protrude through the wall of the vessel. The cone or flow restricting member 31 of each valve is attached to a flexible bellows member or the like 38. and the free end of the valve stem 36 bears against the inner surface of the end of this bellows member to effect adjustment of the position of member 31 in relation to the end of conduit I1 by lowering or raising the valve stem. The bellows member 38 is disposed within a suitable shell or housing 39 and the lower end of the bellows is secured to this housing, its upper end being free to move upon expansion or contraction of the bellows.

Also, in the particular case illustrated, the flow regulating device 2| is of special form employing a iiexible bellows member or the like 40 secured at its lower end to a flange 4I, provided as a closure member for the lower end of conduit I9 and secured at its upper end to a substantially coneshaped element 42 which directs the solid particles from conduit I9 into conduit 20 and restricts flow therebetween to a degree depending upon the proximity of element 42 tothe end of conduit 20. Expansion and contraction of the bellows member 40 with consequent upward and downward movement of element 42 is effected by injecting a suitable fluid into the confined space 43 of the ow control device 2I through line 44, and valve 45 and by withdrawing fluid therefrom through the same line. A similar arrangement for pneumatic or hydraulic control of valves I8 may be substituted, when desired, for the manually adjustable stems 36.oi these valves or member 2| may be arranged for manual adjustment. In fact it is not intended to limit the invention to ilow regulating members of the form illustrated, since many other suitable forms will be readily apparent.

It is also within the scope of the invention to employ separate reaction and regenerating vessels instead of dividing a single vessel, as illustrated, into separate reaction and regenerating zones. However, the regenerating zone is preferably disposed above the reaction Zone or vice versa so that a relatively straight transfer'conduit, like conduit 20, may be employed for the transfer of solid particles from the upper to the lower zone, This avoids excessive wear due to erosion encountered at bends in a transfer line of this type wherein the vapor or gas velocity is relatively high. The use of a relatively short, straight transfer line at this point permits the use of higher velocities and higher transfer rates in a line of given size than can be safely ernployed when the line is relatively long and/or contains one or more bends. By thus reducing wear or erosion in this transfer conduit, which would be caused by the passage of solid particles around a bend in the line at high velocity, excessive attrition of the solid particles is also obviated.

The relatively straight transfer conduits Il and I9 are also important features of the invention which assist in facilitating circulation of the solid particles between the reaction and regenerating zones and help to avoid excessive attrition of the solid particles.. advantage of using relatively straight transfer lines, wherein the velocitysof the solid particles' is relatively low due to the relatively high density of the columns, is not so pronounced as in the high velocity transfer line 20 and the invention is not limitedto the use of the straight transfer lines l1 and i9.

Another feature of the preferred embodiment of the invention illustrated is the relatively simple and compact construction of the apparatus and the elimination of external transfer lines. This latter feature is accomplished, in part, by disposing conduit |9 about conduit 20 and bringing its u-pper end to adjacent the upper extremity of bed 1, so that a suitable pressure head is developed in the latter without extending it beneath the Vessel. This materially reduces-the required overall height of the equipment which in previous installations not employing the features of the invention is ordinarily a minimum of one hundred feet, or thereabouts, above the ground level` I claim:

1. An apparatus in which to effect contact between fluids and subdivided solids which comprises, in combination, two confined contacting zones arranged in superimposed relation, each zone being adapted to retain therein a bed of subdivided solid contact material, means for supplying a separate stream of fluid to each of said zones and for passing the same upwardly in contact with the respective beds at controlled velocity, means' for discharging a resulting stream of fluid fromthe upper portion of each of said beds and from the respective zones, means for transw ferring solid particles between said beds from the upper to the lower zone comprising a conduit leading downwardly from a point of the bed in the upper zone -beneath its upper extremity and communicating at its lower end with the bed in the lower zone, means for transferring solid particles between said beds from the lower to the upper zone comprising a pair of concentric vertical conduits disposed'within said lower zone, the outer of said concentric conduits leading downwardly from a point of the bed in the lower zone beneath its upper extremity into the lower end of the inner of said concentric conduits and said inner conduit communicating at its upper end with said bed in the upper zone, means for passing said stream 'of fluid being supplied to the upper zone through the inner conduit, and means for regulating the rate at which solid particles are passed through said conduits.

2. An apparatus in which to effect Contact between fiuids and subdivided solids which comprises, in combination, two confined contacting zones arranged in superimposed relation, each zone being adapted to retain therein a bed of subdivided solid contact material, means for supplying a separate stream of fluid to each of vsaid However, the

8 zones and for passing the same upwardly in contact with the respective beds at controlled velocity, means for discharging a resulting stream of fluid from the upper portion of each of said beds and from the respective zones, means for transferring solid particles between said beds from the upper to the lower zone lcomprising a substantially straight conduit leading downwardly from a point of the bed in the upper zone beneath its upper extremity and communicating at its lower end with the bed in the lower zone, means for transferring solid particles between said beds from the lower lto the upper zone comprising a pair of concentric vertical conduits disposed within said lower zone, the outer of said concentric conduits leading downwardly from a point vof the bed in the lower zone beneath its upper extremity into the lower end ofthe inner of said concentric conduits and said inner conduit communicating at its upper end with said bed in the upper zone, means for passing said stream of uid being supplied to the upper zone through the inner conduit, and lmeans for regulating the rate at which solid particles are passed through said conduits.

3. An apparatus in which to effect contact between fiuids and subdivided solids which comprises, in combination, two confined contacting zones arranged in superimposed relation, each zone being adapted to retain therein a bed of sub-divided solid contact material, means for supplying a separate stream of fluid to each of said zones and for passing the same upwardly in contact with the respective beds at controlled velocity, means for discharging a resulting stream yof fluid from the upper portion of each of said beds and from the respective zones, means for transferring solid particles between said beds from the upper to the lower zone comprising a substantially straight open-ended conduit leading downwardly from a point of the bed in the upper zone beneath its upper extremity and terminating at its lower end within the lower portion of the lower zone, means for transferring solid particles between said beds from the lower to the upper zonecomprising a pair of concentric vertical conduits disposed within said lower zone, the outer of said concentric conduits leading downwardly from a point of the bed in the lower zone beneathand adjacent its upper extremity into the lower end of the inner of said concentric conduits and said inner conduit communicating at its upper end with said bed in the upper zone, means for passing said stream of fluid being supplied to the upper zone through the inner conduit, and means for regulating the rate at which solid particles are passed through said conduits.

4. An apparatus of the class described cornprising, in combination, a vertically elongated substantially cylindrical vessel having an upper and a lower head and an intermediate partition dividing the vessel into upper and lower compartments, a valved inlet conduit for supplying fluid to the lower portion of the lower compartment, a substantially straight transfer conduit open at its upper end and having pressure reducing means disposed adjacent its lower end, said transfer conduit extending vertically downward within the vessel from said upper to said lower compartment, a second transfer conduit, open at its upper end and provided with pressure reducing means adjacent its lower end, extending vertically within the lower compartment from adjacent said partition to adjacent the lower head of the vessel, a third substantially straight transing vertically from a poi'ntwithinsaid second conduit adjacentl the last named pressure reducpoint in the upper compartment to a point adja-A cent the lower portion of the lower compartment,

Aends and extend- I a pair of concentric vertical conduits disposed within the lower compartment, the outer of said concentric conduits having an open upper end in the upper portion of the lower compartment and the inner of saidl concentric conduits having an open lower end adjacent the lower portion of the lower compartment andcommunicatng` 25 at its upper end with said'upper compartment, means for supplying uid to the lower end of said inner conduit and upwardly therethrough into theupper compartment, and meansfor removing Huid-from the upper compartment. CHARLES H. ANGELL.

nEFERENoEs'cIfrEn l The following references are of record -in the le of this patent: i v

'UNITED STATES PATENTS- Number Name x Date 2,046,816v Fowler et al July 7, 1936 2,212,583 Broderson et al. Aug. 27, 1940 2,302,209 Goddin Nov. 17, 1942 .2,311,564 Munday Feb. 16, 1943 2,347,682 Gunness May 2, 1944 1,380,067 Koch et al; 'May 31, 1921 1,601,938 Campbell Oct. 5, 1926 1,845,058 Pier Feb. 16, 1932 1,989,406 Doolittle Jan. 29, 1935 2,304,128 l Thomas Dec. 8, 1942 l 2,341,193 Scheineman Feb. 8, 1944 2,363,874 Krebs Nov. 28, 1944 y FOREIGN PATENTS Number Country Date Germany v sept. a, 1931 

